Method for producing hydrogen with reduced co2 emissions

ABSTRACT

The present invention relates to a method for producing hydrogen, with reduced carbon dioxide emissions, from a hydrocarbon mixture. In said method, the hydrocarbon mixture is reformed so as to produce a synthetic gas that is cooled, then treated in a shift reactor so as to be enriched with H2 and CO2. Optionally dried, said mixture is treated in a PSA hydrogen purification unit in order to produce hydrogen. The residue is treated by means of partial condensation with a view to capturing CO4 before said residue is sent as fuel to reforming.

The present invention relates to a process for the production of hydrogen in combination with capture of CO₂, in which the mixture of hydrocarbons is reformed to produce a synthesis gas which is cooled, then enriched in H₂ and CO₂, optionally dried, and treated in a PSA hydrogen purification unit to produce hydrogen, the waste product being treated with a view to capturing CO₂; it also relates to a plant suitable for carrying out the process.

Climate change is one of the major current environmental problems; the increase in the concentration of greenhouse gases in the atmosphere, in particular of carbon dioxide, is an essential cause of this. Reducing the emissions of greenhouse gases, and very particularly reducing CO₂ emissions, is one of the major challenges facing mankind.

CO₂ of human origin originates from various sources; each type of emission has to be reduced. One of the essential emissions is, however, that which results from the combustion of fuels, very particularly fossil fuels.

The European Community is committed to achieving a reduction of 8% in its emissions of greenhouse gases between 2008 and 2012, compared with the 1990 level. To help in achieving this result, a market for the emissions of greenhouse gases (ETS, Emission Trading System) has been established. Thus industrial sites have to buy quotas corresponding to their emissions of greenhouse gases and particularly of carbon dioxide.

Units producing hydrogen and carbon monoxide emit carbon dioxide by the combustion of carbon-based fuels. The CO₂ present in the flue gases thus originates from the combustion of gases, not of economic value, generated in the process and recycled in the form of fuels, and of additional fuels, such as naphtha and natural gas.

If they are not yet affected, sites for the production of H₂/CO will be included in the ETS from 2013.

Furthermore, many other countries, such as Canada and the United States, also intend to institute a CO₂ emissions quota market.

Thus, because they will soon be subjected to this constraint, these sites and in particular sites for the production of hydrogen must now develop solutions for capturing CO₂ of high efficiency.

A portion of the CO₂ emitted in the flue gases originates from the combustion of carbon-based fuels recycled from the process; the gases, not of economic value, sent for combustion comprise, in variable proportions, methane, carbon dioxide, nitrogen and also hydrogen.

In order to reduce emissions of CO₂ by the flue gases, one solution consists in treating the flue gases in order to capture the CO₂ downstream of combustion; a second solution consists in reducing the contribution of CO₂ originating from the recycled gases.

It is this second solution which the invention is targeted at improving. This is because the first solution treats flue gases where the CO₂ is diluted in the nitrogen of the combustion air, which makes it more expensive to separate the CO₂.

The purpose of the present invention is to reduce the contribution of CO₂-generating entities originating from the recycled gases, while maintaining the effectiveness of the combustion. It concerns not only reducing the contribution of CO₂ but also reducing the contribution of entities which generate CO₂ by combustion (mainly CO and CH₄).

The invention is of particular use in the specific case of the production of hydrogen.

When it is desired to produce hydrogen from a gas rich in hydrogen—typically a synthesis gas enriched in hydrogen by a high-temperature shift reaction (HT shift) in the presence of steam (according to the reaction CO+H₂O→CO₂+H₂)—, the process used for the separation and the purification of the hydrogen is the pressure swing adsorption (PSA) process. This process makes it possible to generate a stream of pure hydrogen—with a purity generally of greater than 99% by volume—and a waste gas depleted in hydrogen which concentrates the other entities present in the starting mixture to be purified, including CO₂.

A solution currently used to capture the CO₂ present in the process gas consists in recovering it with regard to the waste product from the unit for the purification of the hydrogen, via a compression and purification unit (CPU)—thus before the combustion which dilutes the CO₂ in the nitrogen of the combustion air—. This solution is described in particular in the document WO 2006/054008.

A process for the production of hydrogen has to incorporate a process for capturing CO₂, exhibiting a high CO₂ capture efficiency.

An objective of the invention is thus—in order to reduce the emissions of CO₂ in the flue gases—to convert entities which generate CO₂ into CO₂ not during the combustion but upstream of the recycling, making it possible for the additional CO₂ thus produced to be captured specifically or with the preexisting CO₂.

The carbon dioxide is recovered by treatment of the waste product from the unit for the purification of the hydrogen (pressure swing adsorption unit—PSA H₂). This treatment is carried out in a compression and purification unit (CPU) by cooling the waste product from the PSA until it partially condenses and a liquid rich in carbon dioxide and a new gaseous waste product, comprising the noncondensable compounds resulting from the treatment by the CPU, are obtained.

Until now, attention has been directed at the treatment of the PSA waste product for the purpose of capturing a significant portion of the CO₂ present in the synthesis gas and of thus limiting the emissions of CO₂ in the combustion flue gases; the fact nevertheless remains that the recycling of the waste gases from this capturing treatment—which capturing is generally carried out in a compression and purification unit (CPU)—is capable of also generating an even greater amount of CO₂ in the combustion flue gases, this CO₂ originating from carbon-based molecules other than CO₂ but which can produce CO₂ (essentially CO and CH₄).

In order to improve the efficiency of capture of the CO₂, it is known to treat the noncondensable gases resulting from the CPU by membrane permeation, the aim being to obtain a stream rich in methane in order to recycle a portion thereof in the combustion region of the furnace and a portion in the reforming region.

It is this which is described in the document WO 2006/054008, which teaches a process for the production of hydrogen and for the production of carbon dioxide in combination starting from a synthesis gas obtained by reforming natural gas in which a fluid enriched in carbon dioxide is recovered by treatment of the waste product from the PSA H₂ unit, this treatment making it possible to obtain at least one liquid or supercritical stream rich in CO₂ and a second gas stream rich in H₂ and comprising most of the remaining CO₂; this document additionally discloses treating this second stream in a permeation unit in order to produce two streams, the first of which, which is rich in H₂ and CO₂, will be recycled in the charge feeding the PSA, while the second, which comprises CO, CH₄, N₂, and the like, is sent to the reforming furnace, including the combustion of the flue gases part and the conversion of methane to hydrogen part.

However, with this solution, the methane and the carbon monoxide present in the second stream resulting from the treatment of the waste product from the PSA are still introduced into the burners and thus generate CO₂ by combustion, which is thus still discharged to the atmosphere.

In order to limit the emissions of CO₂, the aim of the invention is to limit the contribution—at the burners—of entities which emit CO₂ by combustion (CH₄, CO and CO₂) and very particularly to eliminate, from the recycling, the entities exhibiting the poorest intrinsic calorific value/carbon dioxide emitted ratio. As is shown in the table below, the entities to be removed from the recycling as fuel are thus, first, carbon dioxide itself, the intrinsic calorific value of which is zero, but also carbon monoxide, the intrinsic calorific value of which is three times lower than that of methane, the most advantageous entity for combustion without emission of CO₂ being, very naturally, hydrogen.

Entities H₂ CH₄ CO CO₂ kcal/Sm³ CO₂ generated ∝ (infinite) 8550 3020 0

For this, the solution of the invention consists in combining individual operations for conversions and/or separations of entities, applied to carefully chosen streams, with the aim of optimizing the capture of CO₂ and thereby of significantly limiting the emissions of CO₂ generated by the partial recycling of the noncondensable waste gases from the compression and purification unit or CPU in the process for the production of hydrogen.

A subject matter of the invention is thus more particularly a process for the production of hydrogen in combination with capture of carbon dioxide starting from a mixture of hydrocarbons, comprising at least the following steps:

-   a step (a) of reforming the mixture of hydrocarbons in order to     obtain a synthesis gas comprising at least hydrogen, carbon     monoxide, carbon dioxide, methane, water vapor and impurities, -   a step (b) of cooling the synthesis gas with recovery of the     available heat, -   a step (c) of a shift reaction on all or part of the cooled     synthesis gas in order to oxidize most of the carbon monoxide to     give carbon dioxide with corresponding production of hydrogen, -   a step (d) of cooling the synthesis gas enriched in H₂ and CO₂     resulting from step (c) with separation of the condensed water, -   an optional step (e) of additional drying of the cooled synthesis     gas in order to obtain a dry synthesis gas (with a water content of     less than 200 ppm), -   a step (f) of separation of the constituents of the dry synthesis     gas in a pressure swing adsorption (or PSA H₂) unit which makes it     possible to obtain a high-pressure stream enriched in hydrogen and a     stream Rpsa of PSA waste gas predominantly comprising carbon dioxide     and hydrogen but also carbon monoxide, methane and impurities,     and also steps of treatment of the stream Rpsa comprising at least: -   a step (g) of compressing said waste stream Rpsa such that its     pressure is between 20 and 100 bar, -   a step (h) of treatment of a stream X resulting—directly or     indirectly—from the stream Rpsa in order to separate CO₂, making it     possible to obtain a stream of liquid or supercritical CO₂ and a     gaseous capture waste product Rc enriched in hydrogen and in other     noncondensable constituents, -   a step (i) of treatment of the capture waste product Rc in order to     produce at least one stream to be recycled as fuel in the reforming     furnace,     characterized in that the process additionally comprises, downstream     of step (f), an additional step (j) of treatment of the stream Rpsa,     which step (j) is situated upstream of a step of separation of CO₂     and which step (j) is a second shift reaction step which can be     followed by removal of water, thus producing a dry gas depleted in     CO and enriched in CO₂ and in H₂.

If need be, step (g) can be preceded by a step of drying the stream Rpsa in order to remove water molecules present in the waste product Rpsa and to thus obtain a waste product Rpsa which is sufficiently dry to prevent the condensation of carbonic acid in step (g).

The stream X treated in step (h) can result directly from the stream Rpsa; in this case, step (j) will be followed by an additional step of separation of the CO₂. The stream X can also result indirectly from the stream Rpsa, that is to say be the product of a treatment to which the stream Rpsa has been subjected—for example a step (j)—, and step (h) forms, in this case, said step of separation of the CO₂ as described above.

The aim of the treatment of the invention is thus to convert the carbon monoxide which was not converted during the first shift reaction of step (c), so as to remove the carbon monoxide which, without this additional treatment, would still be present in the final stream to be recycled. This conversion by a shift reaction with steam is carried out according to the reaction: CO+H₂O<=>CO₂+H₂.

A shift reaction does not provide complete conversion, all the less so when it is carried out at high temperature; it makes possible greater conversion of the CO to CO₂ at moderate temperature (MT shift) and even more at low temperature (LT shift).

The shift reaction of step (c) is generally carried out at high temperature (the outlet temperature is between 250 and 480° C.) since it is applied to the synthesis gas generated at a very high temperature and specially cooled in order to carry out this reaction. There thus remains, at the outlet of step (c), a significant proportion of unreacted carbon monoxide. It is this remaining carbon monoxide which will react subsequently during step (j). The CO₂ thus formed is removed by separation, either alone or at the same as the CO₂ present at the outlet of the first shift step (c), according to the location of this additional step according to the invention. This second shift step, carried out at medium or low temperature (the outlet temperature is between 200 and 300° C.), makes it possible to remove the bulk of the CO, which would be returned as fuel to the reforming, and thus to significantly reduce the amount of CO₂ in the flue gases.

This additional shift step can be carried out in different locations in the process, provided that a step of separation of the CO₂ produced is included in the process downstream. Thus, according to preferred alternative forms:

-   -   step (j) is fed with the compressed waste product Rpsa resulting         from step (g), and the shifted and optionally dried gas         resulting from step (j) constitutes the stream X which feeds         step (h), which step (h) constitutes in this case said step         during which the CO₂ is separated, as described above;     -   step (j) is fed with the capture waste product Rc resulting from         step (h), and the shifted and optionally dried gas resulting         from step (j) is subsequently treated in a step (k) which         separates the CO₂—which will be sent back to feed step (h)—and         produces a gas rich in H₂ capable of being recycled as clean         fuel; preferably, step (k) is a step of pressure swing         adsorption via a PSA CO₂, and then the waste product rich in         hydrogen resulting from said adsorption step is recycled as         clean fuel in the reforming;     -   step (j) can be fed with the permeate enriched in hydrogen, CO         and CO₂ from a membrane downstream of step (h), and the shifted         and optionally dried gas resulting from step (j) is subsequently         recycled at the inlet of step (f) of separation by pressure         swing adsorption.

According to another aspect of the invention, the latter relates to a plant for production of hydrogen combined with capture of carbon dioxide starting from a mixture of hydrocarbons, comprising at least:

-   -   a module for reforming the mixture of hydrocarbons in order to         obtain a synthesis gas,     -   a first module for cooling the synthesis gas with means for         recovering the available heat,     -   a module for shifting the synthesis gas with steam,     -   a module for cooling the shifted synthesis gas with condensation         of the steam and recovery of the condensed water,     -   an optional module for drying the shifted and cooled synthesis         gas,     -   a unit for purification by pressure swing adsorption (or PSA) of         the dry synthesis gas which makes it possible to obtain hydrogen         and a waste product Rpsa,         and also:     -   a compression module capable of compressing the waste product         from the PSA up to a pressure of between 20 and 100 bar,     -   means for carrying out step (h) of treatment of a stream X         resulting (directly or indirectly) from the stream Rpsa in order         to separate CO₂, making it possible to obtain a stream of liquid         or supercritical CO₂ and a gaseous capture waste product Rc         enriched in hydrogen and in other noncondensable constituents,     -   means for treating the capture waste product Rc in order to         produce at least one stream to be recycled as fuel in the         reforming furnace,         and in which the plant additionally comprises, downstream of the         compression module and upstream of a means for separation of the         CO₂, a second shift module which can be followed by a module for         the removal of water.

According to preferred alternative forms, the plant comprises all or some of the following means:

-   -   means for feeding the second shift module with the compressed         waste product Rpsa, and means intended to feed the means for the         implementation of step (h) with shifted gas resulting from the         second shift module which can be followed by a module for the         removal of water;     -   means for feeding the second shift module with the capture waste         product Rc resulting from the means for the implementation of         step (h), and also means for treating the shifted gas resulting         from step (j) in order to separate the CO₂ and to produce a gas         rich in H₂, and also means for feeding the means for the         implementation of step (h) with said separated CO₂, and means         capable of recycling said gas rich in H₂ as fuel;         advantageously, said means for treating the shifted gas         resulting from step (j) in order to separate the CO₂ and to         produce a gas rich in H₂ comprise a unit for the separation of         CO₂ by pressure swing adsorption of the PSA CO₂ type,     -   membrane permeation means for treating the capture waste product         Rc, means for feeding the second shift module with the permeate         enriched in hydrogen, CO and CO₂ resulting from the membrane         permeation means, and means for feeding the unit for the         purification by pressure swing adsorption (or PSA) of the dry         synthesis gas which makes it possible to obtain hydrogen and a         waste product Rpsa with the shifted gas resulting from said         second shift module which can be followed by a module for the         removal of water.

Other characteristics and advantages of the present invention will become apparent on reading the description below of nonlimiting implementational examples, which descriptions are made with reference to the appended figures, in which:

FIG. 1 is a diagrammatic view of a process for the production of hydrogen in combination with capture of carbon dioxide according to the invention, in which the (second) shift step according to the invention is carried out on the waste product resulting from the step of separation of CO₂ by CPU, the product from the reaction being treated by a PSA CO₂,

FIG. 2 is a diagrammatic view of a process for the production of hydrogen in combination with capture of carbon dioxide according to the invention, in which the (second) shift step according to the invention is placed downstream of the separation of hydrogen by PSA and upstream of the step of separation of CO₂ by CPU,

FIG. 3 is a diagrammatic view of a process for the production of hydrogen in combination with capture of carbon dioxide according to the invention, in which the (second) shift step according to the invention is carried out on the permeate from the membrane permeation of the waste product resulting from the step of separation of CO₂ by CPU.

FIG. 1 thus describes a preferred embodiment of the process of the invention in which a charge of hydrocarbons 1 mixed with steam (not represented) feeds a reformer 2 in order to generate a synthesis gas 3 comprising at least methane, hydrogen, carbon monoxide and carbon dioxide. This steam reforming step is carried out in a steam reforming furnace comprising tubes filled with catalysts, the heat necessary for the reforming being contributed by combustion. The synthesis gas 3 is then cooled in 4, the cooled synthesis gas 5 subsequently being subjected in 6 to a shift reaction during which the carbon monoxide reacts with water (represented but not referenced) in order to be—in part—converted into H₂ and CO₂, thus making it possible to improve the production of hydrogen. The reaction involved (CO+H₂O→CO₂+H₂) is known as the shift reaction. The reaction is generally carried out at high temperature in an HT shift (high-temperature shift) reactor. The synthesis gas 7 obtained—enriched in H₂ and in CO₂—is cooled in 8 and then the cooled gas 9 is dried in 10 in order to remove the water molecules and to thus obtain a dry gas mixture 11, which is subjected to a step of separation in a unit 12 for pressure swing adsorption (or PSA H₂), thus making it possible to obtain a high-pressure stream 13, enriched in hydrogen to a purity at least equal to 98%, and a low-pressure waste gas 14, comprising carbon dioxide and also the other gases present in the synthesis gas: CO, CH₄, N₂ and impurities, and also the hydrogen not extracted in the PSA H₂.

The stream 14 is subsequently treated in order to capture the CO₂ therefrom; for this, it is compressed (not represented) so that its pressure is between 20 and 100 bar and then is subjected to one or more successive steps of condensation/separation in the CPU unit 20 in order to obtain a liquid stream 21 enriched in CO₂ and a gas stream (capture waste product Rc) enriched in hydrogen and in other noncondensable constituents, in particular in carbon monoxide.

The gas stream 22 is subsequently subjected (after heating—not represented—up to a temperature of between 190 and 250° C.) to a shift reaction in 23 in a shift reactor operating at low temperature (low-temperature shift or LT shift) in the presence of water (the addition of steam is represented but not referenced). This passage of the capture waste product through the shift reactor thus makes it possible to convert the greater part of the CO present in it into CO₂, in order to capture it, thus limiting the CO₂ content of the flue gases. The shifted gas 24 comprises a mixture of hydrogen, carbon dioxide, methane and nitrogen, with traces of carbon monoxide; it is dried in 25 to produce a dry shifted gas 26, which is subsequently introduced into a separation unit 27. According to the process of FIG. 1, this separation unit is a unit for separation by pressure swing adsorption via a PSA CO₂, which produces a stream 29 enriched in CO₂ and a stream 28, a PSA CO₂ waste stream, very predominantly comprising hydrogen, a large amount of methane, and also carbon dioxide, carbon monoxide and nitrogen as minor constituents. The stream 29 rich in CO₂ is sent to the unit for the capture of CO₂ to be treated therein and the stream 28 is sent as clean fuel (generating little CO₂ in the flue gases) to the reforming unit 2.

FIG. 2 describes a second preferred embodiment of the process of the invention. Some elements common to the 3 embodiments of the invention carry the same reference numbers. The elements which differ carry different numbers. A first part of the process—disregarding the variations in compositions and flow rates due to the recycled streams—up to obtaining the streams 13 and 14 at the outlet of the PSA H₂, referenced 12, is identical in the diagrams of the three figures.

The stream 14 is subsequently compressed in 30 so that its pressure is of the order of 30 bar. The compressed gas stream 31 is subsequently subjected (after heating up to a temperature of between 190 and 250° C.) to a shift reaction in 32 in a shift reactor operating at low temperature (low-temperature shift or LT shift) in the presence of water (not referenced). This passage of the PSA waste product through the shift reactor thus makes it possible to convert the greater part of the CO present therein into CO₂, which will add to that already present in the stream 31. The shifted gas 33 comprises hydrogen, carbon dioxide, methane, nitrogen and traces of carbon monoxide; it is dried at 34 to produce a dry shifted gas which is subsequently subjected to one or more successive steps of condensation/separation in the CPU unit in 36 in order to obtain a liquid stream 38 enriched in CO₂ and a gas stream 37 enriched in hydrogen and in other noncondensable constituents. The stream 38 constitutes the CO₂ produced by the process and the gas stream 37 (stream of the noncondensable products or capture waste product) is enriched in hydrogen. In addition, it comprises the noncondensable constituents, in particular methane, nitrogen and unconverted carbon monoxide but also a nonzero portion of the carbon dioxide.

Depending on the requirements and needs to be satisfied, there will exist various possibilities for the use of this stream 37; specifically, after the shift step according to the invention, the noncondensable products from the CO₂ compression and purification unit essentially comprise CH₄, N₂, if there is some in the reformed mixture of hydrocarbons, and H₂.

Mention will be made, among the uses which can be envisaged, of:

-   -   the use in the reforming furnace as clean fuel; in comparison         with the current solution, this gas exhibits a much lower degree         of emission of CO₂ per unit of heat as it virtually no longer         comprises CO₂ or CO, the intrinsic calorific value of which is         virtually three times lower than that of CH₄,     -   the recycling in the mixture of hydrocarbons upstream of the         reforming region. The CH₄ can thus be converted to hydrogen and         CO. Care must be taken not to accumulate nitrogen in the system         by bleeding off a portion of this gas,     -   the recycling upstream of the PSA H₂, thus making it possible to         increase the production of hydrogen of the system. Care must be         taken this time not to accumulate nitrogen and methane. In this         case, a membrane permeation step is advantageous.

According to the diagram of FIG. 2, the stream 37 is thus treated in 39 by membrane permeation in order to obtain a stream 41 rich in hydrogen, which is recycled upstream of the PSA H₂, and a waste product 40 under pressure. As the nitrogen permeates only to a very small extent with the hydrogen, the recycling of the hydrogen at the inlet of the PSA does not result in an accumulation of nitrogen in the process. The waste product 40 is recycled to the reforming unit, in part as charge, supplementing the charge of hydrocarbons, and in part as fuel.

FIG. 3 describes a third preferred embodiment of the process of the invention. A certain number of elements common to the 3 embodiments of the invention carry the same reference numbers. The elements which differ carry different numbers. The first part of the process—disregarding the variations in compositions and flow rates due to the recycled streams—up to obtaining the streams 22 and 21 at the outlet of the CPU unit, referenced 20, is identical in the diagrams of FIGS. 1 and 3.

The stream 22 is subsequently treated in a membrane permeation module in 42 in order to obtain a stream 43 rich in hydrogen, CO and CO₂ and a waste product 44 under pressure. The stream enriched in hydrogen, CO and CO₂ 43 is subsequently subjected (after heating up to a temperature of between 190 and 250° C.) to a shift reaction in 45 in a shift reactor operating at low or medium temperature in the presence of water (not referenced). This passage of the permeate through the shift reactor thus makes it possible to convert the greater part of the CO present therein into CO₂, which is added to that already present in the stream 43. The shifted gas 46 comprises hydrogen, carbon dioxide and traces of carbon monoxide; it is recycled upstream of the drying unit 10.

The waste product 44 from the membrane permeation unit 42 is treated in 47 by membrane permeation in order to obtain a stream 48 rich in CO₂, which is recycled upstream of the CPU unit 20, and a waste product 49 under pressure. The waste product 49 is recycled to the reforming unit as fuel. 

1-10. (canceled)
 11. A process for the production of hydrogen in combination with capture of carbon dioxide starting from a mixture of hydrocarbons, comprising: (a) reforming the mixture of hydrocarbons in order to obtain a synthesis gas comprising hydrogen, carbon monoxide, carbon dioxide, methane, water vapor and impurities, (b) cooling the synthesis gas with recovery of the available heat, (c) reacting all or part of the cooled synthesis gas in a shift reaction in order to oxidize most of the carbon monoxide to give carbon dioxide in the presence of water with corresponding production of hydrogen, (d) cooling the synthesis gas enriched in H₂ and CO₂ resulting from step (c) with separation of the condensed water, (e) drying the cooled synthesis gas in order to obtain a dry synthesis gas, (f) separating the constituents of the dry synthesis gas in a pressure swing adsorption unit which makes it possible to obtain a high-pressure stream enriched in hydrogen and a stream Rpsa of PSA waste gas predominantly comprising carbon dioxide and hydrogen but also carbon monoxide, methane and impurities, and also steps of treatment of the stream Rpsa comprising at least: (g) compressing said waste stream Rpsa such that its pressure is between 20 and 100 bar, (h) treating a stream X resulting from the stream Rpsa in order to separate CO₂, thereby obtaining a stream of liquid or supercritical CO₂ and a gaseous capture waste product Rc enriched in hydrogen and in other noncondensable constituents, (i) treating the capture waste product Rc in order to produce at least one stream to be recycled as fuel in the reforming furnace, (j) [downstream of step (f)] treating the stream Rpsa, which step (j) is situated upstream of a step of separation of CO₂ and which step (j) is a second shift reaction step which can be followed by removal of water, thus producing a dry gas depleted in CO and enriched in CO₂ and in H₂.
 12. The process of claim 11, wherein step (j) is fed with the compressed waste product Rpsa resulting from step (g) and in that the shifted gas resulting from step (j) constitutes the stream X with feeds step (h).
 13. The process of claim 11, wherein step (j) is fed with the capture waste product Rc resulting from step (h) and in that the shifted gas resulting from step (j) is subsequently treated in a step (k) in order to separate the CO₂, which will be sent back to feed step (h), and to produce a gas rich in H₂ capable of being recycled as clean fuel.
 14. The process of claim 13, wherein step (k) of treatment of the shifted gas resulting from step (j) is a step of pressure swing adsorption via a PSA CO₂ and in that the waste gas rich in H₂ resulting from said step (k) is recycled as clean fuel.
 15. The process of claim 11, wherein step (j) is fed with the permeate enriched in hydrogen, CO and CO₂ resulting from a step of membrane separation downstream of step (h) and in that the shifted gas is subsequently recycled at the inlet of step (f) of separation by pressure swing adsorption.
 16. A plant for production of hydrogen combined with capture of carbon dioxide starting from a mixture of hydrocarbons, comprising at least: a module for reforming the mixture of hydrocarbons in order to obtain a synthesis gas, a first module for cooling the synthesis gas with means for recovering the available heat, a module for shifting the synthesis gas with steam, a module for cooling the shifted synthesis gas with condensation of the steam and recovery of the condensed water, a module for drying the shifted and cooled synthesis gas, a unit for purification by pressure swing adsorption (or PSA) of the dry synthesis gas which makes it possible to obtain hydrogen and a waste product Rpsa, and also: a compression module capable of compressing the waste product from the PSA up to a pressure of between 20 and 100 bar, means for carrying out step (h) of treatment of a stream X resulting from the stream Rpsa in order to separate CO₂, making it possible to obtain a stream of liquid or supercritical CO₂ and a gaseous capture waste product Rc enriched in hydrogen and in other noncondensable constituents, means for treating the capture waste product Rc in order to produce at least one stream to be recycled as fuel in the reforming furnace, downstream of the compression module of step (g) and upstream of a means for separation of the CO₂, a second shift module which can be followed by a module for the removal of water.
 17. The plant of claim 16, which comprises: a means for feeding the second shift module with the compressed waste product Rpsa, and a means for feeding the means for the implementation of step (h) with the shifted gas resulting from said second shift module which can be followed by a module for the removal of water.
 18. The plant of claim 16, which comprises: a means for feeding the second shift module with the capture waste product Rc resulting from the means for the implementation of step (h), a means for treating the shifted gas resulting from step (j) in order to separate the CO₂ and to produce a gas rich in H₂, and also a means for feeding the means for the implementation of step (h) with said separated CO₂, and a means capable of recycling said gas rich in H₂ as fuel.
 19. The plant of claim 18, wherein said means for treating the shifted gas resulting from step (j) in order to separate the CO₂ and to produce a gas rich in H₂ comprise a unit for the separation of CO₂ by pressure swing adsorption of the PSA CO₂ type.
 20. The plant of claim 16, which comprises: a membrane permeation means for treating the capture waste product Rc, a means for feeding the second shift module with the permeate enriched in hydrogen, CO and CO₂ resulting from the membrane permeation means for treating the capture waste product Rc, a means for feeding the unit for the purification by pressure swing adsorption (or PSA) of the dry synthesis gas which makes it possible to obtain hydrogen and a waste product Rpsa with the shifted gas resulting from said second shift module which can be followed by a module for the removal of water. 